Art of cracking hydrocarbon oils



July 17, 1928. 1,677,773

E. c; HERTHEL ET AL OF.,CRACKING HYDROGARBON- OILS Filed' June 22, vwas Sumatra-smety 1 @maak mest @S Hl HI.

INVENTOR 5 Eugene C. ller t/rel BY Tnze: d'6'. Tiff# IM, mmf

ATTORNEYS Julylv', 192s. y

E. C.y HERTHEL `E'I' AL ART' QF CRACKING HYDROCARBON OILS Filed June 22. 1926 2 sheets-sheet 2 INVENTOR aye/7e C Hert/zel 720014;

ATTOR N EYS Panarea July 17 192s. i.

UNITED lSTATES,

yPATENT OFFICE. i

UCENE C. Imafrnnr. AND rnonAs DE CoLoN ".rIrr'r, or CHICAGO, ILLINOIS, As-

sIGNORs 'ro SINCLAIR BEFINING COMPANY,` or NEW YORK, N. Y., A CORPORATION or iuAigrrr:1

Application led June 22,

This invention relates to improvements in 4the cracking of higher boiling hydrocarbon oils, such as, gasoil, to produce therefrom lower boiling hydrocarbon oils, such as `gasoline and pressure distillate.,

This invention relates particularly taimprovements in operations in which hydrocarbon oils are cracked'- by distillation under pressure and in which residual oil withdrawn undistilled from the pressure distillation is expanded at a lower pressure for the further separation of oil constituents as vapors therefrom. The invention has several important advantages in heat'economies, in features of control, and in. the maintenance of conditions A which permit prolongation of the useful period of operation without sacrifice of eiiiciency. The invention is of special value and application in connection with the operation of pressure cracking stills ot the type described in Patent No.A 1,285,200 issued November 19, 1918, to the Sinclair Refining Company on an application to Edward Wr Isom, and it will be described particularly in connection therewith, but in certain aspects it has advantages which areof more general application. l v f In carrying out the present invention, the oil to be cracked is subjected to distillation under pressure at a cracking temperature -in a pressure still, the vapors driven olf from the still are subjected lto a refiuxing operation in a reiuxtower from which relux is returned tothe still, and the vapors remaining uncondensed from the reiuxing operation are condensed to form the 4distillate product. Theoperation is carried out in a continuous manner by supplying fresh oil to the pressure still charge and withf drawing unvaporized oil containing the pitch formed Aby cracking during vthe `operation and regulating the rate of supply of `fresh oil and the rate of Vwithdrawal of pitth-laden Oil so that the concentration of pitch in the still charge is kept below the saturation point. The pitch laden oil withdrawn from the still charge is expanded by reducing the pressure thereon and is thereby separated into an unvaporized residue.

y 'and an oil fraction driven oli as vapors.

The pitch content of 'the unvaporizecl oil withdrawn from the pressure still charge l f A31' OF. CRACKING HYDROCAILBON OILs.

'1926. 'serial No. 117,697.

isseparated in this residue and the oil components of the withdrawn material, or,

the greater part of them, are separated as vapors, thisgseparation. advantageously be- Ing etfecte'd simply byV the heat contained in the pitch-laden oilifrom the pressure still.

In accordance with the present invention, the oil. vapors separated from the pitchladen oil withdrawnl from the pressure still are passed through a tower into which fresh oil to be supplied toA the pressure still is passed 1n directl contact' with these' vapors. The-fresh oil" is thus heated and the vapors are cooled. The heavier components of the 'vapors are condensed and togetherwith the unvaporlzed components of the fresh OiLare then introduced into direct contact with the `vapors inthe reluxin operation to which the vapors driven olf om the pressure still are subJec'ted. In the tower through which th vapors separated from the unvaporized oil wlthdrawn from the pressure still are passed, lighter constituents suchK as those product remain uncondensed and, together with any vsimilar Vconstituents contained in the fresh oil supplied to this tower, areu withdrawn and separately condensed.

The condensate and admixed fresh oil .l

withdrawn from the second tower, the tower through wh-ich the vapors separated from the unvaporized' oil, withdrawn from the pressure still are passed, are advantageously returned to the pressure still in a heated state, either as withdrawn from the tower or ypartially cooled, or they may be returned after cooling approximately to atmospheric temperature. This mixture when introduced hot into the reflux tower through which the vapors from the pressure still are reflux tower on the pressure still may be cooled sufficiently so that it has 1n the reflux tower the desiredl refluxing action and can maintain the temperature of the escaping vapors at the desired point.` In either yof these operations, a part of the heat of the vapors separated from the unvaporized oil withdrawn from the pressure still is rebe supplemented by that of another refluxing a ent in the way that has been described. In a dition -to the fresh oil supplied to the second tower, part of thefresh oil to beosupplied to the operation may be introduced directily into the reflux tower on the pressure stil The operation of the tower, through which the vapors separated from the unvaporized oil withdrawn from the pressure still are passed, is advantageously controlled so that the vapors escaping uncondensed therefrom correspond in character to the pressure distillate escaping as vapors from the reflux tower on the pressure still. These vapors ma thenbe condensed and collected `to get er with the pressure distillate from the pressure still as part of the desired distillate product. This control of the operation of the second tower may be effected by re ulating the rate at which fresh oil is supphed thereto, if the amount of fresh oil required to be supplied to the pressure still operation.

is at least sufficient to effect the necessary condensation, but usually it is advantageous to employ in addition to the fresh oil some supplemental condensing agent. One particularly advantageous way of controlling the operation of this tower is to return and introduce into the tower, best at a point above the point f introduction of the fresh oil,l a part of the pressure distillate in amount regulated so that the vapors escaping are of the desired character. The pressuredistillate, or similar fraction, supplied to the tower to effect the control in this way is substantially completely revaporized escapingr with the vapors from the tower to be condensed therewith.

Fig 1 of the accompanying drawings is a p1ctorial representation of the .operation of the process of the invention. The invention will be further describedl in connection with Flg. 2 of the drawings which illustrate, 1n

a diagrammatic and conventional manner,-

above.

an apparatus adapted for carrying out the process of the invention.

Referring to Fig. 2 of lthe drawings, the pressure still illustrated is of the type described ian Patent No. 1,285,200, referred to The pressure still comprises a'bulk supply tank 30 located away fromthe heating furnace 4, a battery of vertical heating tubes 5 arranged in the heating furnace, and circulating connections 6,/7 and 8 and a circulating pump 9 arranged to withdraw oil from the bulk supply tank and force it upwardly through the heating tubes and back to the bulk supply tank. Vapors from the bulk supply tank 'escape through connection 10 and pass upwardly through the reflux tower 11, uncondensed vapors escaping from the upper end of the reflux tower through connection 12 to the condenser 13 in which they are condensed, the condensate collecting in receiver 14. A connection 15 is provided for the discharge of uncondensed Vvapors and gases and a connection 16 for discharge of the condensate. Reflux, and any admixed unvaporized oil introduced into the reflux tower, are returned from the reflux tower 11 tothe circulating line connecting the bulk supply tank with the suction side of the circulating pump through connection 17. Unvaporized oil Ais with` drawn from the bulk supply tank 3 through connection 18 arranged tofdischarge into the expander 19. A pressure reducingyalve 20 is provided in the connection 18, advantageously at a point adjacentI the /pressure still,to control and reduce the pressure between the bulk supply tank and the expander. To promote vaporization, steam, or

other heated gaseous medium, may be introduced yinto the expander ,19, for example, steam may be injected into and/admixed with the oil as it enters the' expander. 'As little as 1% of steam will, in many cases,

materially increase the amount of vaporiza-V tion over any particular pressuredrop. To inhibit entrainment, several bafiles or other suitable means are arranged in the upper end of the expander 19. Vapors escape from the expander through connection 21 and un-- vaporized material is discharged through connection 22 to the cooler 23. The vapors from the expander pass upwardly through the expander tower 2l, uncondensed vapors escaping from the upper end ofthe tower through connection 25 to the condenser 26 in which they are condensed, the condensate collecting in receiver 27 which is provided with a discharge connection 28 for uncondensed vapors and gases and connection 29 for\ the discharge of condensate. Fresh oil is supplied by means) of pump 30 to theupper end of the expander tower 24 through l lo connections 31 and 32. A part of the fresh v oi-l so supplied may also beintroduced into the upper end of the reflux tower 11 through ing temperature,

connection 33. The condensate and admixed fresh oil collecting in the lower end ofY expander tower 24 is withdrawn through connection 34. This mixture may be introduced into the upper end of the reflux tower 11j through connections 35, 36 and 37 by means of pump 38; or through connection 39, the cooler 40 and connections 41, 36 and 37 by m`eans of pump 38. A' part of the mixture may be returned directly to the circulating connection supplying oil to the lower end of the heating tubes in the pressure still )through connections 42 and 43 by means of pump 44. As a supplemental reluxing or condensing agent or controlling medium, a part of the distillate product can be rein-l troduced by means of pump 45 either into the upper end of the reflux tower 11 through connection 46 or into the upper' end of expander tower 24 through connection 47. fThe hot parts of the apparatus as well as the ht connections are advantageously lagged or heat insulated to prevent heat loss, particularly the expander 19. To promote condensation therein the expander tower 2 4 may be left uninsulated, although control is somewhat facilitated if this tower is also insulated against heat loss.

In the apparatus illustrated, the circulating pump 9 is of the rotary impeller type and connections 48 are provided for forcing -`cool oil through the bearings to protectA them from the high temperature of the hot oil passing through the pump at or near a crackbut a relatively small amount of oil is required, or if desired a much larger proportion of the oil to be supplied to the pressure still' can be introduced in this way. For example, fresh oil may be so supplied through connection 49, or art of the mixture collecting in the expa'n er tower'f 24 may be so supplied through connection 50. lIf the temperature of the mixture from the expander tower is too high to rovide sufficient cooling, er 51 on its way to the pump bearings.

In operation, the, pressure still is charged f with fresh oil and brought to cracking con# Yditionsi of temperature and pressure. In a still of the type illustrated an initial charge of about 8000 gallons of cold oil, that is oil at a temperature of ample, is commonly employed. Thel pressure maintained during the operation is determined to a large measure by the stoc to be treated and the products to be obtained. With gas oil character charging stocks pressures upto 125 pounds r square inch or more may be used and with charging stocks containing large amounts o f kerosene character components v'much higher pressures, say up to 300 pounds per square inch or ,more, may be used. When the still is brought to operating conditions the intro- Simply to effect coolingr it may be passed t rough coolduction of fresh oil through connection 37 .is begun and pressure distillate` vapprs vare discharged into the condenser and condensed, the preure `being regulated by valve 52 `between the reflux tower and thel condenser. vThe pressure may also be regulated, if desired, by valves beyond the condenser. During the initial period of operation, unvapor 'ized oil is not withdrawn from the pressure still, or is withdrawn in but small amount,

but before the pitch concentration in the charge of oil in the pressure still reaches the saturation point the withdrawal of pitchladen oil in substantialamount is begun and the rate. of withdrawal of pitch-laden oil and of supply of fresh oil is regulated to maintain the concentration of pitch in the pressure kstill charge below the saturation point.v The pitch-laden oil withdrawn is discharged into Asure substantially lower than that prevailing within the pressure between the still and the exthe `expander 19 where a presi the pressure still is maintained,

pander being reduced by'means of valve 20.

Due to this reduction in pressure, the withdrawn pitch-laden oil is lsubjected to ur. ther vaporization, the expander tower and pitch components sepa? rating ina residue still remaining unvaporized. The degree of vaporization in the expander can be controlled by regulating the pressure therein. As Amuch as or more gof the pitchladen'oil may be so vaporized by its self-contained heat, residue is to be obtained it is usually not desirable to go muchbeyond this point and it may be necessary to reduce the amount of vapor-ization,

sometimes be obtained with vaporization of as much as of the pitch-,laden oil. Or

but if .a liquid although a liquid residue can` vapors entering the rate a coke or coky residue in which event a.

series of the expanders becomes necessary so 'that the operation can 4be carried out continuously', to permit cleaning and removal of the @time that the pitch-laden oil is'beng subjected to further vaporization under 'reduced pr'eure. @With still pressures in the neighorhood' of 100 pounds lper square inch or higher, the' pressure in the expander may be maintained at a value ,between` atmospheric ressure and say 50 pounds per square inc or higher, depending lon the amount of vaporization desired. When the -withdrawal of pitch-laden oil is begun, and vvapors from this oil begin to pass through the expander tower, the fresh oil, or part of it is introduced'into the top of the expander tower through connection 32 and the oil introduced into the top' o the reflux tower,

through connection 37 is supplied, in whole or in part,A from the oil mixture withdrawn from the lower end of the expander tower.

solid or semi-solid residue at the same Part of' this 011 mixture may ,be supplied130 f of thevoil as withdrawn from the gallons per hour of this oil may be vaporized,

directly to the charge of oil circulating in the out pressure distillation processes for crackpressure still in addition to that introduced ing hydrocarbon oils which effects several into the reflux tower. heat economies. The separation of unvapor- Operating for the production of gasoline, ized oil withdrawn from the pressure disor gasoline-containing pressure' distillate, tillation into a residue containing all of the vwith 'a gas oil -character charging stock, as pitch constituents of the withdrawn oil and an example of the operation of the invention, a -completely vaporized fraction is effected the temperature at the top of the reflux without requiring additional heat, and furtower l1 may be maintained at about 550 ther atleast a part of the heat'of the frac- F. and the temperature at the top of the tion so vaporized is returned to the pressure expander tower 24 at about 350 F. The distillation ins a particularly advantageous pressure distillate may be taken olf at a-rate, way. This heat is absorbed in part in fresh for example, of about 1000 gallons per hour oil which is brought in contact with the `and pitch-laden unvaporized oil withdrawn vapors forming this separated fraction, and

from the still charge at a rate of about 1500 is returned directly to the pressure still in gallons per hour, requiring the return to the the condensate produced from these vapors pressure still of 2500 gallons of oil per hour and in the heated fresh oil. Part of this to maintain the charge. The temperature heat may be given up in cooling of the niixy pressure ture of fresh oil and condensate, but neverstill, during operation under a pressure in theless some of it is returned and made the neighborhood of `100 to 125 pounds per usefully available in the cracking operation Square inch, may approximate 700 to l725 whereas otherwise it would be lost for this F., and on reduction to approximately atniospurpose. Heat so returned to the pressure pheric pressure up to about 80% or 1200 distillation assists in prolonging the period the temperature of ,the vapors and of the as it reduces to a corresponding extent the residue escaping from the expander approx-` amount of heat necessary to be transferred imating 650 F., or upwards. Since part of through the walls of the pressurej still yin this vaporized fraction of the oil withdrawn which the operation is carried out making from the still charge escapes as vapors from possible lower furnace temperatures to effect the expander tower, fresh oil in amount any given conversion of a particular stock. upwards from 1300 gallons per houris sup- Such lower furnace temperatures can be plied. If all of this fresh oil is supplied, maintained efficiently by recycling part of through the expander tower, the tempera? the heating gases again over the heat transture ofthe mixture collecting in the bottom ferring walls. With the withdrawal of subof the expander tower may approximate stantial amounts of pitch-laden oil from they 480 F., and since it is usually desirable to pressure distillation, the economy thus effectture, it is usually advantageous to cool it to gasoline character `flux tower is supplied to the still charge limit the temperature of the fresh oil introed becomes particularly important. Likeduced into the reflux tower to a value not Wise, in carrying out the invention, lighter exceeding about 275 to 280 F., to maintain constituents present in the oil withdrawn adequate refluxing action and a head temfrom the pressure distillation which if reperature approximating 550 F., this mixturned might be subjected to overcracking ture or at least that part of it introduced into are separated before the condensate prothe rcfiux tower, is cooled to this temperaduced'from the vapors separated from this ture, or otherwise some supplementary reoil under reduced pressure is returned to fluxing agent is` employed. Similarly, if the pressure distillation and may be compait of this mixture is supplied to the bearbined with the distillate product; and simiings of the circulating pump 9 to protect larly lighter constituents present in fresh them from the hot oil at cracking temperaoil supplied to the operation,rfor example, constituents present in about 200 F., or less. The supply ofl oil coke-still gasoil charging stock due to the to the reflux tower 11 is regulated to maincracking iiitailed in the operation of the still .tain the desired head temperature, and oil to cokeor gasoline character constituents necessary vto be supplied to the still charge in absorbed in fresh charging stock by treating excess of the amount introduced into the regas mixtures such as the uncondensed vapors and gases from pressure stills or coke-stills directly. The oil so supplied is advantageously returned at as high a temperature as ticularly advantageous way. If stocks conis available. To maintain the desired khead taining such lighter componentsare supplied temperatures, part of the distilled product directly to the pressure still or to a reflux may be supplied to the upper ends of the tower on the pressure still, heat is absorbed reflux tower and the expander tower as in the still in vaporization of such comporequired, l nents, and frequently in over-cracking of It will thus be seen that this invention such components, which otherwise would be provides an improved method of carrying available for useful cracking. In this respect over which the operation can be continued g with the fresh oil, can be separated in a par- Y feired through walls of the pressure the capacityof the pressure still.

also the invention makes it possible to reduce the amount -of heat necessary to be transl-1 sti to effect any given conversion of a particular stock of this type or conversely to increase The invention has another advantage in that the apparatus for cooling the components of the pitch-laden oil, in accordance witltthe iin vent-ion, can be made compact and of a type easily maintained; a tower` with direct heat exchange between vapors froin the pitchladen oil and fresh charging stock or other condensing agent can be made less cumbersome and can be kept in operation morel cooled condensers of coneasily than water ventional construction of adequate size t0 condense the vapors resulting from expansion ofthe oil, or than coolers of conventional construction to bring the withdrawn oil. to a sutiicie-ntly low temperature to handle without vaporization. a

le claim: l. In processes hydrocarbon oils of cracking higher boiling to produce lower boiling 'hydrocarbon oils by distillation under presl a reduced pressure,

sure at cracking temperatures in which iin-Q vapor-ized oil is withdrawn during the pressure distillation and subjected to further vaporization by its self-contained heat under the improvement which comprises passing the vapors separated from the oil withdrawn from the pressure distillation into a tower, introducing fresh oil directly into the vapor space in this tower, so as to bring the fresh oil and vapors into direct and intimate contact therein, thereby subjecting the vapors to condensation, passing the vapors from the pressure still into a reflurt tower and introducing' adlnixed condensate and unvaporized fresh oil from the trst. mentioned tower into direct contact with the vapors therein, and returning reiux together with admixed unvaporized oil fronrthe said" refiuxtower to the pressure distillation.

-a reduced pressure, comprises passingthe vapors separated from pressure disv 2. In processes hydrocarbon oils to produce lower boiling hydrocarbon oils by distillation under presof ycracking higher boiling sure at crac-king temperatures in which unvaporized oil is withdrawn during the pressure distillation and subjected to further faporization by its self-contained heat under the improvement which the oil withdrawn from the tillation4 into a tower, introducing fresh oil directly into the vapor space in this tower so as to bring the fresh oil and vapors into direct and intimate contact therein, thereby subjecting the vapors to condensation, passing the vapors from the pressure still into a redux tower and first mentioned tower while still in a heated stateltherefrom into direct contact with the vapors in the said reflux tower, and returning reflux together with adinixed unvaporized oil introduced into the said reflux tower to the pressure distillation.

3. In processes of cracking higher boiling `hydrocarbon oils to produce lower boiling hydrocarbon-oilsby distillation under pres-4 sure at cracking temperatures in which unoil is Withdrawn during the pres# EUGENE O. HERTHEL. THOMAS DE COLON TIFFT.

introducing admixed condensate and unvapoi'ized fresh oil from the DISCLAIMER 1,677,77'3.Eugene` O. Herz/hel vand Thomas De Colon Ti't, Chicago', vIll. ART oir CRA'CKING HYDROCARBON OiLs. Patent dated .July 17 1928. Disclaimer filed described in claims 1, 2 and 3 of said specification as limited to processes: i

, Wherein the distillation under pressure recited in the `cl ims is a primary pressure distillation to which is supplied at least some fresh oil Wherein the pressure on the unvaporized oil that is Withdrawn during the pressure distillation and subjected to further vaporization by its self-cpntained heat is reduced from the pressure at Which the prnnary pressure distillation iseffected in aly Single stage and Without'intermediate distillation to a pressure lower than the pressure maintained in said distillation under pressure by an amount suiicien't to produce A v aporization of a substantial part of said oil Withdrawn during the pressure distillation by its self-contained heat. v

.y Wherein a condensateis formed in the tower into Which vapors separated from the 011 Withdrawn from the pressure distillation are passed, and such condensate at least y said oil withdrawn during the pressure distillation remaining unvaporized;

nd,v wherein the said further Vaporizati'on of unvaporized oil Withdrawn from the primary pressure distillation is eected entirely or substantially entirely by its -selfcontained heat.

[Oficial Gazette May 10, 1.932.] J n 

